CN102959072B - Method and system for the gas tight process control of percolators in biogas method having two or more stages - Google Patents
Method and system for the gas tight process control of percolators in biogas method having two or more stages Download PDFInfo
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- 238000000034 method Methods 0.000 title claims abstract description 106
- 238000004886 process control Methods 0.000 title description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 446
- 239000007788 liquid Substances 0.000 claims abstract description 122
- 239000000463 material Substances 0.000 claims abstract description 67
- 230000000035 biogenic effect Effects 0.000 claims abstract description 43
- 239000007787 solid Substances 0.000 claims abstract description 35
- 238000010926 purge Methods 0.000 claims abstract description 30
- 230000007062 hydrolysis Effects 0.000 claims abstract description 22
- 238000006460 hydrolysis reaction Methods 0.000 claims abstract description 22
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 131
- 238000000354 decomposition reaction Methods 0.000 claims description 120
- 238000003860 storage Methods 0.000 claims description 67
- 238000011084 recovery Methods 0.000 claims description 22
- 239000011159 matrix material Substances 0.000 claims description 20
- 238000000855 fermentation Methods 0.000 claims description 11
- 230000004151 fermentation Effects 0.000 claims description 11
- 238000011068 loading method Methods 0.000 claims description 11
- 244000005700 microbiome Species 0.000 claims description 9
- 230000009089 cytolysis Effects 0.000 claims description 3
- 239000012530 fluid Substances 0.000 abstract description 3
- 239000007789 gas Substances 0.000 description 241
- 238000011026 diafiltration Methods 0.000 description 50
- 230000008569 process Effects 0.000 description 42
- 239000003570 air Substances 0.000 description 38
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 22
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 18
- 230000000875 corresponding effect Effects 0.000 description 15
- 239000002253 acid Substances 0.000 description 14
- 238000010408 sweeping Methods 0.000 description 13
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- 238000013461 design Methods 0.000 description 10
- 239000001301 oxygen Substances 0.000 description 10
- 229910052760 oxygen Inorganic materials 0.000 description 10
- 239000000047 product Substances 0.000 description 9
- 235000011089 carbon dioxide Nutrition 0.000 description 8
- 239000001569 carbon dioxide Substances 0.000 description 7
- 229910002092 carbon dioxide Inorganic materials 0.000 description 7
- 238000006243 chemical reaction Methods 0.000 description 7
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- JYYOBHFYCIDXHH-UHFFFAOYSA-N carbonic acid;hydrate Chemical compound O.OC(O)=O JYYOBHFYCIDXHH-UHFFFAOYSA-N 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 150000004666 short chain fatty acids Chemical class 0.000 description 4
- 239000000243 solution Substances 0.000 description 4
- 239000007921 spray Substances 0.000 description 4
- 239000000758 substrate Substances 0.000 description 4
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 3
- 230000002411 adverse Effects 0.000 description 3
- 230000015556 catabolic process Effects 0.000 description 3
- 239000007857 degradation product Substances 0.000 description 3
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- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 230000003301 hydrolyzing effect Effects 0.000 description 2
- 235000016709 nutrition Nutrition 0.000 description 2
- 231100000616 occupational exposure limit Toxicity 0.000 description 2
- 239000011368 organic material Substances 0.000 description 2
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- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 150000001413 amino acids Chemical class 0.000 description 1
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- C12M43/00—Combinations of bioreactors or fermenters with other apparatus
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- C12M21/00—Bioreactors or fermenters specially adapted for specific uses
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- C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
- C12M29/02—Percolation
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- C12M45/00—Means for pre-treatment of biological substances
- C12M45/06—Means for pre-treatment of biological substances by chemical means or hydrolysis
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- C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
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Abstract
The invention relates to a method and a system for obtaining biogas in two or more stages in a hydrolysis and a methane stage, wherein the hydrolysis of solid biogenic materials is performed in at least two percolators operated at offset times. Liquid hydrolyzate and CO2 rich hydrolysis gas, and then hydrolysis gas comprising methane thereby arises in the percolator. The liquid hydrolyzate is removed from the percolators, wherein part of the hydrolyzate is fed into the methane stage and the other part of the hydrolysis stage. In the methane stage, the hydrolyzate is converted to biogas and fermenting fluid. In the method according to the invention, the percolators are operated in a gas tight manner and hydrolysis gas is drawn off from the percolators, wherein the hydrolysis gas comprising methane is fed to an energy utilization and CO2 rich hydrolysis gas is used for purging a further percolator operated at an offset time. The system according to the invention is suitable for performing said method and comprises at least two gas tight percolators that are interconnected by means of the gas supply lines thereof, and at least one methane reactor.
Description
Technical field
The present invention relates to the method and system for diafiltration solid biologic source material in the biogas method with two or more grades.The present invention is applicable to the renewable energy resources and produces field.
Background technology
Biogas equipment is utilized to occur from renewable starting material, the refuse that can biological obtain and other material produce biogass, in the apparatus the microorganism biogas that becomes to be made up of main ingredient methane and carbon dioxide by described material biotransformation.
Biodegradable (hereinafter referred to as " biogenic ") material transition becomes biogas to occur in several biochemical steps, is namely hydrolyzed, produces acid, produces acetic acid and methane phase.
In hydrolysis, water soluble ingredient is from biogenic material dissolves, but not water-soluble biological source material is decomposed into water miscible, usual low molecular material by many perienzymes.In order to accelerate some decomposition course, so-called outside enzyme can also be used.In follow-up product acid, the material dissolved during being hydrolyzed is converted into short chain organic acid, such as short chain fatty acid and amino acid.During product acetic acid, organic acid is converted into acetic acid, forms CO in this process
2.The product producing acetic acid utilizes methanogen to be converted into methane during methane phase.
In single-stage biogas equipment, these processes are parallel generation in the time and space.In two-stage biological gas methods, be hydrolyzed and be separated on operation technique equipment with process with methanogenic sub-step (second stage) with product acetic acid with the sub-step (first step) of producing acid.Thus likely to control respectively during being hydrolyzed and varying environment condition in the conversion process that occurs respectively during methane phase.This causes the stability of level of control raising and method higher.Therefore, the biogas method of two or more grades can produce the methane concentration higher than single-stage biogas method in biogas.Along with hydrolytic process is technically separated, various matrix can be changed, make the modular design of biogas equipment become possibility.
In existing language usage, the first step of two-stage biological gas methods is often called hydrolysed grade for short, and the second stage is called as methane stage.Hydrolysed grade occurs in so-called hydrolysis reactor.Methanation occurs in so-called methane reactor.The aqueous solution after hydrolysis is commonly called hydrolyzate.Hereinafter, by the language usage according to simplification.
In hydrolysis reactor, biogenic material is broken down into short chain organic acid, forms water decomposition gas simultaneously.Usually, this water decomposition gas is discharged from process, does not use during the course further.
For unhydrolyzed solids biogenic material, various method is all applicable.Except the hydrolysis in stirred-tank reactor or plug flow fermentor, the method for diafiltration is utilized to be general.In diafiltration, solid biologic source material is deposited in hydrolysis reactor, so-called percolator, and sprays with liquid (process water).The liquid formed during diafiltration, it, with organic acid (hydrolyzate, herein also referred to as percolate), is transported in temporary storage tank by from percolator.Be stored in the hydrolyzate in corresponding hydrolyzate tank, be admitted in a controlled manner in methane reactor.In the reactor, the methanogen under anaerobic survived forms the biogas containing methane.This feeding controls to make likely to control methanogenesis.According to the knowledge condition of present stage, methanogenesis occurs in two ways, and namely changed by acetic acid nutritional type and hydrogen nutritional type, the two runs parallel in methane reactor.The organic substance comprised in hydrolyzate thus be transformed into methane and be transformed into other by product.Remaining liquid does not have the organic breakdown products of biogenic material to a great extent, is referred to as fermented liquid.This fermented liquid is discharged from methane reactor.
The hydrolysis of solid biologic source material is well known in the prior art, and utilizes so-called aerobic diafiltration (being also called " open diafiltration " or " open hydrolysis ") to perform herein.It is contrary with the Anaerobic cultural methods of airtight percolator must be had, the possibility having airflow to enter in aerobic diafiltration, therefore there is the aerobic possibility being transformed into carbonic acid gas and water of organic constituent, directly enter the possibility of air with gas, cause the water decomposition gas of potential biogas formation and formation to continue the loss of overflowing.The water decomposition gas existed during aerobic operation mainly containing carbonic acid gas, and can comprise other gas of a small amount of hydrogen, methane and trace, such as H
2s.
WO 2006/048008 and WO 2007/012328A1 both describes two-stage biological gas methods, wherein performs aerobic diafiltration, makes the water decomposition gas formed to escape into air.The aerobic turnover of biogenic material causes the formation of carbonic acid gas and water to increase, therefore matrix can energy content adversely reduce.
Except the biogas formed by methanation, the water decomposition gas formed during diafiltration also part can comprise methane.This especially limit or prevent supply diafiltration oxygen time occur.
In open diafiltration, any methane of formation can escape into air.This produces biogas both shortcomings for economical and ecological.It causes increasing greenhouse gases to the pollution of air, and because the methane of respective amount no longer can be used for energy recovery, so reduce energy output.In addition, being entered by the oxygen during aerobic diafiltration, facilitate that biogenic material is aerobic is decomposed into carbonic acid gas and water, there is the power loss with this biogas process in it.
If in a gastight manner perform diafiltration and thus restriction or stop any oxygen to enter in percolator completely, then organic constituent transforms in anaerobism mode.The two-stage biological gas methods that anaerobism diafiltration occurs is known, such as, comes from DE 102006009165A1.DE 102006009165A1 discloses and produces the method for biogas from the refuse two-stage containing organic materials and be suitable for the reactor of operation of this method.Described percolator is stuffy, makes hydrolytic process control only to occur in anaerobism mode.Thus the water decomposition gas formed is discharged from percolator and is wasted.
Anaerobism by means of used organic materials transforms, and the methane concentration in water decomposition gas can reach than level higher during aerobic diafiltration during anaerobism diafiltration.Known method adds methanogenesis microorganism by inoculation to hydrolysed grade, so as to allow to have produced during the hydrolysed grade of aerobic percolation process in energy can methane.
In addition, can realize being converted into methane by increasing the residence time of hydrolyzate in hydrolysed grade.For this reason, DE 102008007423A1 discloses two-stage biological gas methods and corresponding system, and water decomposition gas is transformed into heat energy at least partly by this.The heat energy produced from water decomposition gas is used to bear the fractional energy requirement produced in described biogas equipment.But, if low and simultaneously its CO of the methane content of water decomposition gas
2content is high, and this hot purposes of water decomposition gas is disadvantageous, because rare gas element needs power consumption conveying in this case.
The inner methane concentration of percolator increases, once again introduce oxygen, just may produce flammable gaseous mixture.In the running of percolator, need the security relationship investigating this situation.In the percolator of gas-tight design, if there is the water decomposition gas with the methane concentration that security is correlated with, the safety dumping of described water decomposition gas is necessary.In addition, fully should reducing the methane concentration of percolator internal gas, especially before emptying percolator, thus flammable atmosphere can be eliminated when opening described tank.
Therefore, the gas (being also called herein " atmosphere " of percolator) comprised in percolator usually before opening described percolator by utilizing gas flare to burn it to get rid of.For this reason, in most of the cases need the another kind of energy using common combustion type, because described gas usually only can not be burnt.
In order to avoid the methane of the percolator effusion security critical concentration from described gas-tight design, known solution reduces the methane concentration in water decomposition gas.
EP 1301583B1 discloses the biogas equipment being designed for and being carried out single-stage methanation by dry fermentation, and itself feature is its outstanding security.In order to realize this object, described equipment configuration measures the sensor of oxygen partial pressure in fermentor tank.If oxygen partial pressure exceedes certain ultimate value, it sends signal, and oxygen is entered by leakage.Biogas pipe is closed automatically, utilizes equipment from biogas the waste gas sent to and form primarily of carbonic acid gas.The gas existed in fermentor tank can be overflowed by purging valve, makes finally to stay almost to only have carbonic acid gas in tank.
EP 2103681A2 discloses the solution further developed of the system as EP 1301583B1, wherein uses the carbonated waste gas from comprehensive heating power-supply unit (CHP) to drive away the biogas containing methane from the dry fermenting process of single-stage.By doing like this in single biogas equipment, fermented substrate above (fermentation (solid biologic source material changes into biogas from methane and carbon dioxide anaerobism) of (Aerobic processes) and compost, and unnecessary matrix is diverted to compost can be performed simultaneously.This method is consisted of such mode: in single-stage biogas production process, before fermentation ends, and the removing of fermentor tank gas phase is occurred by the carbonated waste gas supplied at the end of fermenting process from CHP.The methane concentration being present in the gas in fermentor tank utilizes sensor determination.If the methane content of gas exceedes certain ultimate value (utilizing described gas to carry out energy recovery when this ultimate value just meaningful), described gas is admitted to CHP.If described value is lower than this ultimate value, described gas is discharged by gas flare and is burnt, and this can comprise the fuel that supply is added.If the methane content of gas continues lower than lower the second ultimate value (can allow from fermentor tank safety discharging air when this value), fresh air replaces carbonated waste gas to be admitted to fermentor tank, is discharged in environment by described gaseous mixture by biogas vapor pipe simultaneously.By supplied fresh air, also composting process may be run in the system.
Disclosed in EP 1301583B1 and EP 2103681A2, system and method represents single-stage biogas production process, and its shortcoming is that the methane concentration produced in biogas is restricted.In addition, particularly in working method disclosed in EP 2103681A2, energy expenditure is needed to be rich in CO
2waste gas send reactor back to from CHP, thus decrease total energy generation efficiency in such a system.
Summary of the invention
The object of this invention is to provide the method and system obtaining biogas with two-stage, wherein can utilize the gas formed during being hydrolyzed better.
According to the present invention, by method unhydrolyzed solids biogenic material at least two percolators run with offset time of the acquisition biogas of two or more grades, solve this purpose, wherein said method comprises a hydrolysed grade and a methane stage.Therefore biogenic material is hydrolyzed in hydrolysed grade, thus in percolator, form hydrolyzate liquid and water decomposition gas.In this process, CO is rich in formation
2the first water decomposition gas, then formed containing the water decomposition gas of methane.Remove hydrolyzate from described percolator and collect, thus making a part of hydrolyzate be admitted to methane stage, another part hydrolyzate is admitted to hydrolysed grade.In methane stage, hydrolyzate is converted into biogas and fermented liquid by methanogenesis microorganism.From methane reactor, remove fermented liquid and collect, optionally being sent into hydrolysed grade.In the method for the invention, percolator runs in a gastight manner, and water decomposition gas is extracted out from described percolator.By doing like this, be used to energy recovery containing methane water decomposition gas, and come from a percolator be rich in CO
2water decomposition gas be used to purge another runs (in percolator purging) percolator with offset time.
Observe the methane forming increasing amount during the present invention is based on the diafiltration of solid biologic source material, especially close at the end of diafiltration process, but when diafiltration process starts, formed and there is CO at high proportion
2water decomposition gas.
In the method for the invention, this is due to the microbial growth of generation natural in matrix and development and occurs owing to adding (process control of this liquid is also referred to as respective liquid " circulating operation " in this article) caused by hydrolyzate and fermented liquid during hydrolysed grade.Be admitted to the hydrolyzate of hydrolysed grade and fermented liquid from the storage tank being arranged in hydrolysed grade downstream (hydrolyzate storage tank) or methane stage downstream (fermented liquid storage tank).
Methanogenesis microorganism is sent into hydrolysed grade from methane stage by this, it does not have oxygen in the airtight percolator of hydrolysed grade, the organic constituent of hydrolyzate is changed into methane.In the method for the invention, do not perform inoculate methanogenesis microorganism in hydrolysed grade.The methanogenesis microorganism be present in percolator is present in matrix, or is admitted in percolator by adding fermented liquid.In the method for the invention, hydrolyzate is directly discharged from hydrolysed grade.Preferably, do not take measures increase the residence time of hydrolyzate in hydrolysed grade, this by facilitation of hydrolysis thing component in hydrolysed grade to methane conversion.The hydrolysising by-product that the methane formed in the hydrolysed grade of the inventive method causes as described process and being formed.
The processing condition of the inventive method are intended to by the abundant solute transport of water-soluble organic compounds from used solid biologic source material in hydrolyzate liquid, and this occurs by means of microorganism or enzymatic conversion process.This realizes preferably by acidity operation (pH value of hydrolyzate is in acid range).Preferably, this operating under controlled slight oxygen supply (slightly aerobic) occurs.
Method of the present invention is the biogas production method of two or more grades, and it comprises hydrolysed grade and methane stage, thus only in hydrolysed grade, there is solid biologic source material.In hydrolysed grade, by the conversion process decomposing organism source material of microorganism and enzyme, from described biogenic material eluting water dissolubility organic constituent.These components send solution of anhydrating to together with liquid, aqueous, form hydrolyzate.In the methane stage of the inventive method, organic constituent is by means of only hydrolyzate, be namely admitted to by liquid, aqueous.In the method for the invention, there is not biogenic solid in optimization methane level.
When performing the inventive method with more than one percolator, described percolator is in parallel or be connected in series on hydrolyzate controls.In the sense of the present invention, percolator to be connected in parallel the hydrolyzate referring to and remove from each percolator merged before being admitted to methane stage.In the sense of the present invention, being connected in series of percolator refers to that the hydrolyzate removed from a percolator is admitted to the liquid inlet opening of its adjacent percolator, and this percolator is preferably just equipped with biogenic material at time point comparatively early.
Ratio (the especially CO of component in water decomposition gas
2and methane) depend on the solid biologic source material (matrix) of use.
The water decomposition gas under anaerobic formed when diafiltration process starts is rich in CO
2, and be further characterized in that its methane content is low.This part water decomposition gas is also referred to as in this article and is rich in CO
2water decomposition gas.Be rich in CO
2water decomposition gas preferably there is the CO of at least 50 volume %, preferably at least 70 volume %
2content, and be less than 2 volume %, be preferably less than the methane content of 0.5 volume %.When diafiltration process starts, the pH value of hydrolyzate at slightly acid range, preferably at pH4 to pH5.Now, during the course because methane content is low, water decomposition gas is utilized to carry out energy recovery nonsensical.Due to CO
2content is high, and this part water decomposition gas is suitable for other percolator purged in this process.
Along with the conversion of biogenic material during anaerobism diafiltration is in progress, the methane content of water decomposition gas increases, and its CO
2content reduces.This part water decomposition gas is also referred to as in this article " containing methane water decomposition gas ".Containing the preferred CO of methane water decomposition gas
2content is less than 70 volume % and methane content is at least 2 volume %, preferably at least 8 volume %.Increase simultaneously with the methane content of water decomposition gas, the pH value of hydrolyzate rises to slightly acid to neutral range; Now in diafiltration process, pH value is preferably at pH>5.Now, in this process, extracted out by method of the present invention containing methane water decomposition gas, and for energy recovery.
In order to energy recovery, optionally processed and purify containing methane water decomposition gas, and for carrying out in the universal process of energy recovery from biogas, such as in CHP as heated air, for supplying Sweet natural gas network, or for by burning running engine.Preferably by utilizing the known gas scrubbing of prior art state and/or pressure swing absorption process to perform processing.By doing like this, can reduce containing the associated gas content in methane water decomposition gas, preferably its CO
2content and/or its H
2s content.
The replacement scheme reclaimed as directly utilizing energizing quantity, was admitted to methane reactor containing methane water decomposition gas before energy recovery, or it and the biogas that formed in methane reactor merge.Thus can prevent the high-amplitude wave of methane content in biogas from moving.
Reclaim containing methane water decomposition gas energizing quantity to utilize, in the method for the invention, described diafiltration is designed to perform in a gastight manner, and namely percolator is closed and is equipped with tracheae, described tracheae allows controlled feeding and the extraction of gas, such as, by valve or gas flap valve.
The diafiltration utilizing method of the present invention to carry out solid biologic source material is included in a percolator and preferably performs following operation steps according to chronological order:
A. percolator is loaded biogenic material (in this article also referred to as percolator charging),
B. exhaust mode,
C. gas Land use models,
D. described percolator is purged with the exhaust of the percolator run with offset time from another,
E. percolator described in air purge is used,
F. percolator is opened.
In exhaust mode, be rich in CO
2water decomposition gas as exhaust extract out from percolator.Exhaust mode runs when diafiltration starts, as long as the water decomposition gas formed contains high CO
2content.Therefore, preferred exhaust mode is in operation lasting, until the methane concentration of gas existed in described percolator reaches the ultimate value that specifies above and/or until the pH value of hydrolyzate reaches the ultimate value specified above.The ultimate value of methane concentration is that matrix is dependent, and is preferably at least 1 volume % methane, more preferably at least 2 volume % methane.If when preferably the methane content of water decomposition gas is at least 8 volume %, water decomposition gas energizing quantity is utilized to reclaim meaningful.The ultimate value of the pH value of hydrolyzate is also that matrix is dependent, mostly preferably most is pH5.
That extracts out from percolator in exhaust mode is rich in CO
2water decomposition gas be admitted to another percolator (it runs and will be purged under offset time) as sweeping gas.In the method for the invention, not intending utilization is rich in CO
2water decomposition gas energizing quantity reclaim.
Then exhaust mode is gas Land use models.In gas Land use models, water decomposition gas is extracted out and for energy recovery from percolator.Gas Land use models runs when there is time point when containing methane water decomposition gas in described percolator during diafiltration process.Preferably, gas Land use models continuous service, until the total amount of the water decomposition gas formed or the methane concentration of gas that exists in described percolator are respectively lower than their ultimate value specified above.Water decomposition gas containing methane is extracted out also subsequently for energy recovery from percolator.For this purpose, optionally it and the biogas formed in the methane stage of biogas method of the present invention are merged.
During purging in steps d operation, first the water decomposition gas be present in percolator is driven away it by feeding sweeping gas and is removed.As sweeping gas, use the exhaust of another percolator run under comfortable offset time, it is punctual at this moment operates with exhaust mode.Therefore need at least two percolators run with offset time, wherein at least one percolator is in exhaust mode.Therefore, " running with offset time " is appreciated that as at least two percolators loading solid biogenic material under different initial time in meaning of the present invention, and experiences their Matrix lysis, makes at least one percolator be in exhaust mode.
As long as the atmosphere of percolator contains the methane concentration that is enough to be utilized on energy and described methane concentration in percolator indicates at least safety critical limit value, then this atmosphere is used for gas and utilizes (energy recovery).During the purging of steps d, the methane concentration in percolator atmosphere reduces.Preferably, purge and continue until the gas volume existed in percolator there occurs complete exchange, and the methane concentration in the atmosphere of percolator is fully reduced to lower than safety critical limit value.The safety critical limit value of methane concentration is preferably lower than 1 volume %, and the 20%(being more preferably methane Lower Explosive Limit (LEL) is equivalent to about 0.88 volume %).
Therefore, during purging, the methane content in percolator atmosphere reduces, and the CO in described atmosphere
2content increases.As long as the methane content of described gas exceedes the ultimate value specified above, then the water decomposition gas containing methane of displacing is used to energy recovery.Because the methane content of gas continues to reduce described in purge, when methane content is too low, such gas energizing quantity is utilized to reclaim nonsensical.Therefore described gas preferably declines extract out from percolator lower than during its methane concentration ultimate value specified above at it, and is not used in energy recovery.In order to this time point in discrimination process, the methane content of the gas existed in monitoring, the preferably described percolator of continuous monitoring.
In order to reduce the content of sweeping gas in percolator, before percolator is opened with air purge it.For this reason, ambient air is admitted to percolator, and it displaces the gaseous mixture of sweeping gas and water decomposition gas from percolator.
After purging, percolator is optionally opened and can be emptying and again load fresh biogenic material subsequently.Preferably as the methane concentration in percolator and CO
2when concentration is all reduced to the threshold value lower than specifying above, open.Described methane concentration is preferably less than 50% of occupational exposure limit (OEL), that is, and preferably approximately 0.5 volume %.
The time length of diafiltration depends on the biogenic material of use.Preferably, the time length (completing above-mentioned process steps a. to f.) of a diafiltration is less than 30 days, is preferably 14 to 25 days.Wherein, exhaust mode is dominant and selects the first five to the Ninth Heaven.When purging percolator, the water decomposition gas containing methane existed in percolator to be purged then operates and displaces it with the exhaust of the percolator of exhaust mode running and remove under carrying out comfortable offset time.
Just directly unidirectional in order to ensure the gaseous interchange between the percolator connected at that time, namely towards percolator to be purged, the percolator just run with exhaust mode operated under offset time preferably closed gas side before purging percolator to be purged, made to produce overvoltage in this percolator (it is in exhaust mode).Subsequently, the exhaust carrying out the percolator operated under comfortable offset time is admitted to percolator to be purged, preferably after reaching pressure threshold.This pressure threshold is higher than interior pressure existing in percolator to be purged.Preferably, compare with percolator internal pressure to be purged, described pressure threshold is at least more than 5mbar pressure; Therefore the water decomposition gas (percolator to be purged) avoided containing methane enters and operates just with the percolator of exhaust mode running under offset time, and the water decomposition gas (percolator to be purged) avoided containing methane enters air when extracting out as exhaust.
The present invention is also included in two or more grades the system obtaining biogas, and it is suitable for performing method of the present invention.
The system obtaining biogas in two or more grades of the present invention comprises at least two percolators, especially solid percolator, and each have a hydrolyzate delivery pipe and a liquid inlet opening.The hydrolyzate delivery pipe of percolator is connected with at least one methane reactor by least one hydrolyzate storage tank.
Percolator in present system in hydrolyzate control with in parallel or be connected in series.When percolator is connected in parallel, the hydrolyzate delivery pipe of percolator is preferably connected with at least one hydrolyzate storage tank, and the percolate from different percolator is merged wherein.The feature of the percolator be connected in parallel is shared liquid inlet opening.Alternatively, or additionally, each percolator downstream preferred arrangements divides other hydrolyzate storage tank (being referred to herein as " the pre-storage tank of hydrolyzate "), and the pre-storage tank of described hydrolyzate is connected with the hydrolyzate storage tank of described system respectively by a liquid line.
When percolator is connected in parallel, the hydrolyzate delivery pipe of described percolator, preferably by the pre-storage tank of hydrolyzate, is connected with the liquid inlet opening of adjacent percolator, and described adjacent percolator is loaded with biogenic material at time point comparatively early.
At least one fermented liquid storage tank connected by fermentation liquid draining pipe of the arranged downstream of at least one methane reactor described.In the system of the present invention, described hydrolyzate storage tank is connected with the respective liquid opening for feed of percolator with fermented liquid storage tank.This permission part hydrolyzate and/or fermented liquid are admitted in percolator as the process water be hydrolyzed.If comprise several methane reactor in the system of the present invention, so they preferably connect with identical hydrolyzate storage tank and/or fermented liquid storage tank with hydraulic fluid side.
In the system of the present invention, percolator is designed to be bubble-tight and each at least one closable feed tube and at least one closable gas discharge pipe of comprising.Each percolator is connected with the methane transducer of the methane content for measuring the gas be present in percolator.This sensor preferably is contained in the measuring apparatus for mensurated gas composition quality and quantity, and described device is connected with corresponding percolator.In addition, each percolator is connected with pH sensor, and described sensor is for measuring the pH value of the liquid be present in corresponding percolator.
In present system, the closed feed tube of percolator is designed to allow to switch to supply air or supplying purging gas.Described at least two percolators are connected to each other by their feed tube, during making under offset time operation, can occur by from be in exhaust mode percolator be rich in CO
2water decomposition gas send in percolator to be purged.For this reason, the feed tube of the two all switches to sweeping gas supply, makes these two percolators to carry out atmosphere exchange.
Each percolator in present system is provided with described feature (having the resistance to air loss design of closable feed tube and gas discharge pipe, methane transducer).System of the present invention comprises at least two, more preferably at least three percolators.
Percolator is that prior art is known.They comprise grid or filter screen bottom, and biogenic material deposits thereon.In addition, they comprise the opening for feed of process water or percolate, and percolate outlet.Percolator for present system seals in a gastight manner and comprises closable feed tube and closable gas discharge pipe, this make only after specially opening could with environment exchanging gas.Therefore, which avoid and treat that the biogenic material of diafiltration continues to be exposed to oxygen-containing atmosphere, by promotion, they resolve into carbonic acid gas and water for this.The formation that oxygen-free atmosphere facilitates the low molecule organic product required for methanation increases.
Close the tracheae (gas supply pipe and gas discharge pipe) being preferably designed for tubular form, implement preferably by the valve be arranged on described supply and delivery pipe or gas flap valve.
Percolator in present system preferably comprises closable gas discharge pipe, and it is designed to allow to carry out in the system (air utilization system) of energy recovery or in gaseous emission to air or close described gas discharge pipe and switch to from containing the water decomposition gas of methane at gaseous emission.Gaseous emission is that prior art is known to the different corresponding solutions of instrument that utilizes.For this reason, described gas discharge pipe preferably comprises the custom-designed valve or the gas flap valve that allow switching.More preferably, gas discharge pipe is arranged closable two-way valve is for this object.
Preferably, described air utilization system is the heat and power supply equipment of present system, the equipment (CO of production biological methane
2washing) or the combination of methane reactor.Preferably, before gas-holder is placed on described air utilization system.
System of the present invention is designed such that the liquid inlet opening of percolator is suitable for hydrolyzate and fermented liquid to send into described percolator.For this purpose, described liquid inlet opening is connected with hydrolyzate storage tank and fermented liquid storage tank.What this feature of present system allowed liquid (that is, hydrolyzate, fermented liquid) in the methods of the invention circulates operation.
System of the present invention comprises at least two, the percolator of preferred at least three gas-tight design, their are in parallel or be connected in series and gas supply pipe each other by them connects, during making under offset time operation, can occur from exhaust mode a percolator be rich in CO
2water decomposition gas be admitted to percolator to be purged.In the percolator be connected in parallel by hydrolyzate delivery pipe, hydrolyzate liquid is collected and merges (hydraulic fluid side is connected in parallel) in hydrolyzate storage tank.To discharge from a percolator and in another percolator operated being fed in offset time being connected in series hydrolyzate in percolator, and percolator below has been loaded with biogenic material at time point comparatively early, with to be connected in series percolator contrary, when being connected in parallel, the hydrolyzate liquid from each percolator is merged.
Percolator is connected to each other by the closed tracheae of the corresponding feed tube representing percolator.Described gas supply pipe is closable, and is designed to allow to switch to air supply or from the gas supply of another percolator or closed described feed tube.Due to this design, controlled gaseous interchange can be had between percolator.Preferably, valve or gas flap valve serve as closure member.
Described percolator operates under offset time, namely with the loading of preferred equally spaced interlace mode generation fresh bio source material.The hydrolyzate liquid formed in percolator is removed from corresponding percolator by hydrolyzate delivery pipe, is placed in hydrolyzate storage tank.Therefrom, a part of described liquid is admitted to the methane reactor of present system.
In other vote of the present invention, pressure transmitter arranged by each percolator, for measuring the pressure of described percolator inside.
System operation of the present invention is as follows:
At least two percolators loading solid biogenic material under offset time, then closes.By liquid inlet opening, to spray and by described solid biologic source material (i.e. matrix) with circulating the process water (i.e. hydrolyzate and fermented liquid) that runs in operation.By sending in liquid, the degradable components of described matrix is transformed into alcohol, sugar and short chain fatty acid, thus is transformed into water-soluble form.The degradable components being dissolved in the matrix in liquid hydrolyzate is removed from described percolator by hydrolyzate delivery pipe.Solid substrate is stayed by grid or filter screen bottom.
By the liquid from hydrolyzate storage tank and/or fermented liquid storage tank is sent in percolator through liquid inlet opening, realize circulating operation.Then, described hydrolyzate is admitted to hydrolyzate storage tank, then sends into methane reactor continuously, and the fermentation of the biogas containing methane and carbon dioxide occurs wherein.
The resistance to air loss of percolator is closed prevents any atmosphericoxygen to enter described percolator, and stops any water decomposition gas to be overflowed from described percolator in uncontrolled mode.
During diafiltration, form water decomposition gas, its chemical constitution changes in diafiltration time.After described percolator loads biogenic material, when diafiltration starts, formed and be rich in CO
2water decomposition gas.Along with diafiltration continues, the CO of water decomposition gas
2content reduces.Meanwhile, the methane content of described water decomposition gas increases.During this process, originally, form organic acid together with the converted product of other material as biogenic material, make the pH value of percolate be acid.Along with diafiltration is carried out, pH value rises to slightly acid to neutral range.
In percolator, preferably perform following operation steps:
Exhaust mode: what formed in percolator inside when diafiltration starts is rich in CO
2water decomposition gas can not be used for energy recovery and be processed through gas discharge pipe from percolator.At this time point, the pH value of hydrolyzate is highly acid.Valve in gas discharge pipe is opened, and water decomposition gas is processed from described percolator as exhaust.
Gas Land use models: in further diafiltration process, forms the methane of increasing amount, the methane content of water decomposition gas is increased, while its CO
2content reduces.If the methane content of the water decomposition gas measured by the methane transducer in measuring apparatus exceedes the ultimate value of regulation, switch gas discharge pipe so as follows, described mode makes described gas discharge pipe be connected with air utilization system.Preferably, before this, water decomposition gas to be collected in storage tank and to process in gas treatment equipment.At this time point, the pH value of hydrolyzate is in neutral to slightly acid scope.
Purge with sweeping gas: at the end of diafiltration, the organic degradation product being present in the biogenic material in hydrolyzate only has a small amount of outlet by hydrolyzate to be removed.The pH value that the pH value in hydrolyzate exit presents close to liquid inlet opening place.The pH value of this liquid utilizes the pH sensor measurement in liquid inlet opening and hydrolyzate delivery pipe.But the methane content of water decomposition gas continues very high.Contain methane water decomposition gas in order to what be left from percolator expeling, the feed tube that the exhaust from another percolator (running under offset time relative to percolator to be purged) is in release position by valve is admitted to as sweeping gas.By the relief valve in gas discharge pipe, the gaseous mixture formed by water decomposition gas and sweeping gas is sent in air utilization system by from percolator.
Once the methane concentration of the inner gaseous mixture formed by the sweeping gas of water decomposition gas and feeding of percolator reaches the lower value specified above, just start air purge process.In percolator, therefore the methane concentration of gaseous mixture is measured by described measuring apparatus.
With air purge: ambient air is sent to by feed tube.The gas composition existed in percolator is measured by measuring apparatus.Once the methane of described measuring apparatus mensuration and CO
2concentration all reach the minimum value specified above, this represents, and described percolator can be opened, emptying and again load.This new loading indicates by exhaust mode, gas Land use models, purges, with air purge and the beginning of opening the new circulation formed with sweeping gas.
Method of the present invention allows in process, utilize the water decomposition gas that can not be used for the different piece of energy recovery (to be namely rich in CO
2water decomposition gas), utilize its to purge the percolator that runs under offset time.
In addition, use method of the present invention, the water decomposition gas part containing methane may be used for energy recovery.By the methane content existed in monitoring water decomposition gas, and pass through gas (that is, methane, the CO according to wherein comprising
2) use different water decomposition gas Land use models, the CO not being suitable for energy recovery of considerable part can be prevented
2enter biogas stream.In addition, by doing like this, prevent the methane being suitable for energy recovery from invalidly escaping in air at biogas production period.This ensure that on the one hand the economic utilization of the biogenic material of conversion improves, and also stops the gas containing methane to be overflowed described percolator in uncontrolled mode when airtight percolator is opened, thus applies security risk or adversely affect weather.On the other hand, the part by separating water decomposition gas is rich in CO
2part, improve the energy content of coarse biometric gas in whole system, it utilizes for further gas and provides advantage.
Utilize at the water decomposition gas being designed to be formed in bubble-tight corresponding percolator, improve and reduce them and in energy, be adversely converted into carbonic acid gas in percolator and water in these there is advantage realizing the conversion to the biogas being suitable for Energy harvesting of the biogenic material that uses.
Therefore, the method of the application of the invention, or corresponding system of the present invention, compared with having the standard biologic gas methods of one or two-stage, make likely to obtain higher methane production from the biogenic material used, and the safety of biogas equipment and the operation of environmental sound.
If described method performs in the equipment comprising several methane reactor, the performance of described method and this equipment so can also be controlled more neatly.As required, such as, according to the amount of the biogenic material used, can close or the adjusting function that comes by switching methane reactor.In described equipment, quiet run is possible, even if because a methane reactor closes (such as keeping in repair), described operation still can continue.
Accompanying drawing explanation
Describe the present invention in more detail according to figure below and exemplary embodiment, but do not limit the invention thereto.
Fig. 1: the CO of the percolator inside of present system
2with the figure that methane concentration and pH value develop.
Fig. 2: use method of the present invention to obtain the schematic diagram of four the airtight percolators be connected in parallel in the system of biogas in point two-stage.
Fig. 3: use method of the present invention to obtain the schematic diagram of four the airtight percolators be connected in series in the system of biogas in point two-stage.
Fig. 4: use method of the present invention to obtain the schematic diagram of four the airtight percolators be connected in parallel in the system of biogas in point two-stage, described system has two methane reactor.
Fig. 5: use method of the present invention to obtain the schematic diagram of four the airtight percolators be connected in series in the system of biogas in point two-stage, described system has two methane reactor.
Embodiment
Embodiment 1: point two-stage obtains the system of the present invention of biogas, has four percolators be connected in parallel
System of the present invention comprises four hydrolysis reactor (P
1-P
4), be solid percolator in this case, as shown in Figure 2, and a methane reactor.Described percolator (P
1-P
4) close in a gastight manner, each percolator contains a feed tube (3) and a gas discharge pipe (4), and they are in the top of each percolator, preferably on the opposite sides.
Each percolator (P
1-P
4) (9) at the bottom of grid or filter screen being equipped with, deposition treats the solid biologic source material of diafiltration thereon.In addition, each percolator (P
1-P
4) comprise liquid inlet opening (1) on its top, send by it the liquid spraying solid biologic source material to.Each percolator (P
1-P
4) grid or filter screen at the bottom of below (9), arrange corresponding hydrolyzate delivery pipe (2).Liquid inlet opening (1) and hydrolyzate delivery pipe (2) both eachly to connect with a pH sensor (14,15), described sensor is for measuring the pH value of the liquid existed in described pipe.
Described percolator (P
1-P
4) hydrolyzate delivery pipe (2) be connected to each other, and to be connected by hydrolyzate storage tank (S) with methane reactor (M).Between hydrolyzate storage tank (S) and methane reactor (M), place valve (19), its adjustment according to it allows liquid flow in methane reactor (M) or flow in percolator (P) (by liquid inlet opening (1)).
Methane reactor (M) comprises biogas delivery pipe (21).Fermented liquid storage tank (G) is arranged in the downstream of methane reactor (M) through fermentation liquid draining pipe (18).
Percolator (P
1-P
4) liquid inlet opening (1) be connected with fermented liquid storage tank (G) and hydrolyzate storage tank (S).In liquid feeding (1), arrange that pH sensor (15) measures the pH value sending into liquid.In addition, valve (20) is disposed in and is arranged in liquid inlet opening (1).
Feed tube (3) is equipped with valve (8) and can opens or closes wittingly, makes ambient air can enter described pipe.Each percolator (P
1-P
4) feed tube (3) be connected to each other, each feed tube (3) is close to entering each percolator (P
1-P
4) opening part there is gas flap valve (10), it can be opened respectively.By opening the gas flap valve (10) of two percolators, gaseous interchange mutual between these two percolators can be allowed.
Each percolator (P
1-P
4) respective gas discharge pipe (4) be connected with measuring apparatus (5), described measuring apparatus (5) is for measuring corresponding percolator (P
1-P
4) the property quality and quantity of internal gas, and measure percolator (P
1-P
4) methane content of the inner gas existed.Each gas discharge pipe (4) is branch, and is equipped with two valve elements (11,12) separately, and it is connected with the different function units of described system.
Valve (11) is connected with the pipe of guiding into for carrying out system (air utilization system) (6) of energy recovery from the water decomposition gas containing methane, thus the storage tank optionally just put into if necessary containing the water decomposition gas of methane and/or gas processing plants.
Valve (12) vent fan (13) of respectively hanging oneself is connected with exhaust system (7).This allows to extract exhaust out.
Each percolator (P
1-P
4) be equipped with pressure transmitter (17).
Described system operation is as follows: percolator (P
1-P
4) loading solid biogenic material under offset time.Close corresponding percolator (P
1-P
4).By liquid inlet opening (1), spray with the percolating liquid (i.e. percolate and fermented liquid) circulating operation operation and pass through percolator (P
1-P
4) in solid biologic source material (i.e. matrix).By sending in liquid, the degradable components of described matrix is transformed into alcohol, sugar and short chain fatty acid, thus is transformed into water-soluble form.The degradable components being dissolved in the matrix in liquid hydrolyzate is removed from described percolator by hydrolyzate delivery pipe (2).Solid substrate is by percolator (P
1-P
4) grid or filter screen at the bottom of (9) stay.
By percolator (P will be sent into from the liquid of hydrolyzate storage tank (S) and/or fermented liquid storage tank (G) through liquid inlet opening (1)
1-P
4), realize circulating operation.
Then, hydrolyzate is transferred to hydrolyzate storage tank (S).Therefrom, it or be used again to diafiltration and (passed through liquid inlet opening (1) and send into percolator (P
1-P
4)) in or it in shunting, be continuously fed into methane reactor (M), be fermented into the biogas containing methane and carbon dioxide wherein.
At the end of diafiltration, the amount of the organic constituent of biogenic material dissolves in hydrolyzate reduces.Therefore several percolator (P
1-P
4) load under offset time, and merged in hydrolyzate storage tank (S) by the hydrolyzate that each hydrolyzate delivery pipe (2) is flowed out.Do like this and guarantee to occur the organic breakdown products of biogenic material to send into continuously in methane reactor.
Utilize percolator (P
1-P
4) gas-tight design, prevent atmosphericoxygen from entering percolator (P
1-P
4) and the effusion of uncontrolled water decomposition gas.
Water decomposition gas is by gas discharge pipe (4) removing.By the methane and carbon dioxide content existed in measuring apparatus (5) monitoring water decomposition gas.
Exhaust mode: when diafiltration starts, water decomposition gas is rich in CO
2.At this time point, the pH value of hydrolyzate is highly acid.Valve (12) is opened and is started vent fan (13).From percolator (P
1-P
4) extract out and be rich in CO
2water decomposition gas.
Gas Land use models: in further diafiltration process, forms the methane of increasing amount, the methane content of water decomposition gas is increased, while its CO
2content reduces.If the methane content of the water decomposition gas measured by measuring apparatus (5) exceedes the ultimate value of regulation, so shut-off valve (12) open valve (11).The water decomposition gas being rich in methane is admitted to air utilization system (6).Preferably, it to be collected in advance in storage tank and to be processed in gas processing plants.At this time point, the pH value of hydrolyzate is in neutral to slightly acid scope.Described pH value is by percolator (P
1-P
4) each pH sensor (14) measure.
Purge with rare gas element (sweeping gas): at the end of diafiltration, the organic degradation product being present in the biogenic material in hydrolyzate is only had and is removed by hydrolyzate outlet (2) on a small quantity.The pH value that the pH value that hydrolyzate exports (2) place presents close to liquid inlet opening (1) place.The pH value of this liquid is measured by pH sensor (14,15).But, still form the water decomposition gas of small amount, but comprise obvious methane content (water decomposition gas containing methane).In order to from percolator (P
1) drive away (namely replace) remaining water decomposition gas containing methane, utilize and carry out operation under comfortable offset time and now with another percolator (P that exhaust mode runs
2) be rich in CO
2exhaust (be rich in CO
2water decomposition gas).
For this reason, first manually or utilize program control system to close percolator (P
1) gas flap valve (10).With percolator (P
1) the valve (12) that connects of air utilization system (6) stay open.
Percolator (P
2) valve (11) close (valve (12) also cuts out), make percolator (P
2) in pressure start due to the continuous generation of gas increase.Pressure transmitter (17) measures, preferably measures percolator (P continuously
2) pressure of interior gas system.If the pressure of described gas system exceedes the threshold value specified above, so percolator (P
1and P
2) gas flap valve (10) open.Percolator (P
1and P
2) therefore connect in front end.
Due to percolator (P
2) inner overvoltage, there occurs from percolator (P
2) gas be switched directly to percolator (P
1) in.By the valve (12) opened, from percolator (P
1) gaseous mixture be transported to air utilization system (6).
Once at percolator (P
1) in be rich in CO by water decomposition gas and inflow
2the methane concentration of gaseous mixture that formed of gas reach the lower value specified above, then valve (12) cuts out.Percolator (P
1) in gaseous mixture methane concentration therefore by measuring apparatus (5) measure.
If methane concentration does not reach lower value, valve (12) also can manual-lock.
With air purge: close percolator (P
3, P
4) air supply flap valve (10), unless they are in identical process stage.Open percolator (P
1) valve (11) and feed tube (3) on valve (8); But present ambient air is sent to by feed tube (3).
Connect vent fan (13), for extracting percolator (P out
1) the middle gas existed.Percolator (P is measured by measuring apparatus (5)
1) in gas composition.Once the concentration of the methane that measures of measuring apparatus (5) and rare gas element reaches the respective minimum value specified above, (optimization methane is less than 1 volume %, preferred CO
2be less than 1.5 volume %), this instruction percolator (P
1) can open, emptying and newly load.
This new loading indicates by exhaust mode, gas Land use models, purges and open the beginning of the new circulation formed.
Embodiment 2: point two-stage obtains the system of the present invention of biogas, has four percolators be connected in series
System of the present invention comprises four hydrolysis reactor (P
1-P
4), be solid percolator in this case, as shown in Figure 3, and a methane reactor.Described percolator (P
1-P
4) close in a gastight manner, each percolator contains a feed tube (3) and a gas discharge pipe (4), and they are in the top of each percolator, preferably on the opposite sides.
Percolator (P
1-P
4) (9) at the bottom of grid or filter screen being respectively equipped with, deposition treats the solid biologic source material of diafiltration thereon.In addition, each percolator (P
1-P
4) comprise liquid inlet opening (1) on its top, send by it the liquid spraying solid biologic source material to.Each percolator (P
1-P
4) grid or filter screen at the bottom of below (9), arrange corresponding hydrolyzate delivery pipe (2).Hydrolyzate delivery pipe (2) is connected with pH sensor (14) separately, and described sensor is for measuring the pH value of the liquid existed in described pipe.
Percolator (P
1-P
3) hydrolyzate outlet (2) separately connect the pre-storage tank (V of hydrolyzate
1-V
3).Percolator (P
2) liquid inlet opening (1) be connected to the pre-storage tank (V of hydrolyzate
1).Correspondingly, percolator (P
3) liquid inlet opening (1) be connected to the pre-storage tank (V of hydrolyzate
2), and percolator (P
4) liquid inlet opening (1) be connected to the pre-storage tank (V of hydrolyzate
3).
Percolator (P
4) hydrolyzate outlet (2) be connected to methane reactor (M) by hydrolyzate storage tank (S).Arrangement of valves (19) between hydrolyzate storage tank (S) and methane reactor (M), its adjustment according to it allows liquid flow in methane reactor (M) or flow in percolator (P) (by liquid inlet opening (1)).
Methane reactor (M) comprises biogas delivery pipe (21).Fermented liquid storage tank (G) is arranged in the downstream of methane reactor (M) through fermentation liquid draining pipe (18).
Percolator (P
1) liquid inlet opening (1) be connected with fermented liquid storage tank (G) and hydrolyzate storage tank (S).In liquid inlet opening (1), arrange that pH sensor (15) measures the pH value sending into liquid.In addition, valve (20) is arranged in liquid inlet opening (1).
Feed tube (3) is equipped with valve (8) and can opens or closes wittingly, makes ambient air can enter described pipe.Each percolator (P
1-P
4) feed tube (3) be connected to each other, each feed tube (3) is close to entering each percolator (P
1-P
4) opening part there is gas flap valve (10), it can be opened respectively.By opening the gas flap valve (10) of two percolators, gaseous interchange mutual between these two percolators can be allowed.
Each percolator (P
1-P
4) respective gas discharge pipe (4) be connected with measuring apparatus (5), described measuring apparatus (5) is for measuring corresponding percolator (P
1-P
4) the property quality and quantity of internal gas, and measure percolator (P
1-P
4) methane content of the inner gas existed.Each gas discharge pipe (4) is branch, and is equipped with two valve elements (11,12) separately, and it is connected with the different function units of described system.
Described valve (11) is connected with the pipe of guiding into for carrying out system (air utilization system) (6) of energy recovery from the water decomposition gas containing methane, thus the storage tank optionally put into containing the water decomposition gas of methane and/or gas processing plants.
Valve (12) vent fan (13) of respectively hanging oneself is connected with exhaust system (7).This allows to extract exhaust out.
Each percolator (P
1-P
4) be equipped with pressure transmitter (17).
Described system operation is as follows: percolator (P
1-P
4) loading solid biogenic material under offset time.In this process, percolator (P is first loaded
4), then order loads percolator (P according to this
3-P
1).Each percolator (P
1-P
4) close after loading.
By liquid inlet opening (1), spray with the percolating liquid (i.e. percolate and fermented liquid) circulating operation operation and pass through percolator (P
1-P
4) in solid biologic source material (i.e. matrix).By sending into described liquid, the degradable components of matrix is converted into alcohol, sugar and short chain fatty acid, thus is converted into water-soluble form.The degradable components being dissolved in the matrix in liquid hydrolyzate is removed from percolator by hydrolyzate delivery pipe (2).Utilize percolator (P
1-P
4) grid or filter screen at the bottom of (9) retain solid substrate.
By percolator (P will be sent into from the liquid of hydrolyzate storage tank (S) and/or fermented liquid storage tank (G) through liquid inlet opening (1)
1), realize circulating operation.Due to being connected in series of percolator, being fed in comparatively early time point from the hydrolyzate of a percolator removing in all cases and being loaded with another percolator of biogenic material.Therefore, from percolator (P
1) hydrolyzate by the pre-storage tank (V of hydrolyzate
1) be transported to percolator (P
2) in.Percolator (P is sent to for by liquid
3) and (P
4) in, also there is corresponding process.
From percolator (P
4) hydrolyzate be transferred to hydrolyzate storage tank (S).Therefrom, it or be used again to diafiltration and (passed through percolator (P
1) liquid inlet opening (1) send into (P
1) in) or it be continuously fed in shunting in methane reactor (M), be fermented into the biogas containing methane and carbon dioxide wherein.
At the end of diafiltration, the amount of the organic constituent of biogenic material dissolves in hydrolyzate reduces.Therefore several percolator (P
1-P
4) load under offset time.Do like this and guarantee to occur the organic breakdown products of biogenic material to send into continuously in methane reactor.
Utilize percolator (P
1-P
4) gas-tight design, prevent atmosphericoxygen from entering percolator (P
1-P
4) neutralize the effusion of uncontrolled water decomposition gas.
Water decomposition gas passes through gas discharge pipe (4) from percolator (P
1-P
4) removing.By the methane and carbon dioxide content existed in measuring apparatus (5) monitoring water decomposition gas.
Exhaust mode: when diafiltration starts, water decomposition gas is rich in CO
2.At this time point, the pH value of hydrolyzate is highly acid.Valve (12) is opened and is started vent fan (13).From percolator (P
1-P
4) extract out and be rich in CO
2water decomposition gas.
Gas Land use models: in further diafiltration process, forms the methane of increasing amount, the methane content of water decomposition gas is increased, while its CO
2content reduces.If the methane content of the water decomposition gas measured by measuring apparatus (5) exceedes the ultimate value of regulation, so shut-off valve (12) open valve (11).The water decomposition gas being rich in methane is admitted to air utilization system (6).Preferably, it to be collected in advance in storage tank and to be processed in gas processing plants.At this time point, the pH value of hydrolyzate is in neutral to slightly acid scope.Described pH value is by percolator (P
1-P
4) each pH sensor (14) measure.
Purge with rare gas element (sweeping gas): at the end of diafiltration, the organic degradation product being present in the biogenic material in hydrolyzate is only had and is removed by hydrolyzate outlet (2) on a small quantity.The pH value that the pH value that hydrolyzate exports (2) place presents close to liquid inlet opening (1) place.The pH value of this liquid is measured by pH sensor (14,15).But, still form the water decomposition gas of small amount, but comprise obvious methane content (water decomposition gas containing methane).
In order to from percolator (P
2) drive away (namely replace) remaining water decomposition gas containing methane, utilize and carry out operation under comfortable offset time and now with another percolator (P that exhaust mode runs
1) be rich in CO
2exhaust (be rich in CO
2water decomposition gas).
For this reason, first manually or utilize program control system to close the gas flap valve (10) of percolator (P2).With percolator (P
2) the valve (12) that connects of air utilization system (6) stay open.
Percolator (P
1) valve (11) close (valve (12) also cuts out), make percolator (P
1) in pressure start due to the continuous generation of gas increase.Pressure transmitter (17) measures, preferably measures percolator (P continuously
1) pressure of interior gas system.If the pressure of described gas system exceedes the threshold value specified above, so percolator (P
2and P
1) gas flap valve (10) open.Percolator (P
2and P
1) therefore connect in front end.
Due to percolator (P
1) inner overvoltage, there occurs from percolator (P
1) gas be switched directly to percolator (P
2) in.By the valve (12) opened, from percolator (P
2) gaseous mixture be transported to air utilization system (6).
Once at percolator (P
2) in be rich in CO by water decomposition gas and inflow
2the methane concentration of gaseous mixture that formed of gas reach the lower value specified above, then valve (12) cuts out.Percolator (P
2) in gaseous mixture methane concentration thus by measuring apparatus (5) measure.
If methane concentration does not reach lower value, valve (12) also can manual-lock.
With air purge: close percolator (P
3, P
4) air supply flap valve (10), unless they are in identical process stage.Open percolator (P
2) valve (11) and feed tube (3) on valve (8); But present ambient air is sent to by feed tube (3).
Connect vent fan (13), for extracting percolator (P out
2) the middle gas existed.Percolator (P is measured by measuring apparatus (5)
2) in gas composition.Once the concentration of the methane that measures of measuring apparatus (5) and rare gas element reaches the respective minimum value specified above, (optimization methane is less than 1 volume %, preferred CO
2be less than 1.5 volume %), this instruction percolator (P
2) can open, emptying and newly load.
This new loading indicates by exhaust mode, gas Land use models, purges and open the beginning of the new circulation formed.
Embodiment 3: point two-stage obtains the system of the present invention of biogas, has four percolators be connected in parallel, has two methane reactor
Described system comprises four hydrolysis reactor (P
1-P
4), be solid percolator in this case, as shown in Figure 4, and two methane reactor.The design and implementation example 1 of described system is similar, and operates in an identical manner.But the difference between the system of this system and embodiment 1 is to arrange two methane reactor (M
1, M
2).They be disposed in hydrolyzate storage tank (S) downstream and by respective methane reactor (M
1, M
2) hydrolyzate opening for feed is connected with it.By valve (19), hydrolyzate can be switched and send methane reactor (M to
1) in or methane reactor (M
2) in.Each methane reactor (M
1, M
2) all comprise biogas delivery pipe (21).Fermented liquid storage tank (G) is through methane reactor (M
1, M
2) fermentation liquid draining pipe (18) be disposed in the downstream of described methane reactor.
Between working life, the hydrolyzate from hydrolyzate storage tank (S) is admitted in a methane reactor.Fermented liquid is from methane reactor (M
1, M
2) be transported in fermented liquid storage tank (G).
Embodiment 4: point two-stage obtains the system of the present invention of biogas, has four percolators be connected in series, has two methane reactor
Described system comprises four hydrolysis reactor (P
1-P
4), be solid percolator in this case, as shown in Figure 5, and two methane reactor.The design and implementation example 2 of described system is similar, and operates in an identical manner.But the difference between the system of this system and embodiment 2 is to arrange two methane reactor (M
1, M
2).They be disposed in hydrolyzate storage tank (S) downstream and by respective methane reactor (M
1, M
2) hydrolyzate opening for feed is connected with it.By valve (19), hydrolyzate can be switched and send methane reactor (M to
1) in or methane reactor (M
2) in.Each methane reactor (M
1, M
2) all comprise biogas delivery pipe (21).Fermented liquid storage tank (G) is through methane reactor (M
1, M
2) fermentation liquid draining pipe (18) be disposed in the downstream of described methane reactor.
Between working life, the hydrolyzate from hydrolyzate storage tank (S) is admitted in a methane reactor.Fermented liquid is from methane reactor (M
1, M
2) be transported in fermented liquid storage tank (G).
Reference numerals list
(1) liquid inlet opening
(2) hydrolyzate outlet (hydrolyzate delivery pipe)
(3) feed tube
(4) gas discharge pipe
(5) measuring apparatus of the property quality and quantity of mensurated gas composition
(6) air utilization system
(7) exhaust system
(8) valve
(9) at the bottom of grid or filter screen
(10) gas flap valve
(11) valve
(12) valve
(13) vent fan
(14) pH sensor
(15) pH sensor
(16) valve
(17) pressure transmitter
(18) fermentation liquid draining pipe
(19) valve
(20) valve
(21) biogas delivery pipe
(G) fermented liquid storage tank
(M) methane reactor
(M
x) comprise the methane reactor of the system of x methane reactor, x>=1
(P) percolator
(P
n) comprise the percolator of the system of n percolator, n>=1
(S) hydrolyzate storage tank
(V) the pre-storage tank of hydrolyzate
(V
n) comprise the pre-storage tank of hydrolyzate of the system of n the pre-storage tank of hydrolyzate, n>=1
Claims (8)
1. in two levels, obtained the method for biogas with the solid biologic source material in the percolator of offset time operation at least two by hydrolysis, wherein run with offset time and refer at least two percolators loading solid biogenic material under different initial time, and experience their Matrix lysis, at least one percolator is made to be in exhaust mode, the method comprises hydrolysed grade and methane stage, wherein biogenic material is hydrolyzed in hydrolysed grade, wherein in described percolator, form liquid hydrolyzate and water decomposition gas, wherein first formed and be rich in CO
2water decomposition gas and then formed containing the water decomposition gas of methane, and wherein hydrolyzate removes from percolator and collects, wherein a part of hydrolyzate is admitted to methane stage, another part hydrolyzate is admitted to hydrolysed grade, thus the hydrolyzate in methane stage is converted into biogas and fermented liquid by methanogenesis microorganism, and described fermented liquid removes and collects from described methane reactor, and be optionally admitted to hydrolysed grade, it is characterized in that described percolator operates in a gastight manner and the operation of percolator comprises operation steps in the following order:
A. percolator is loaded biogenic material,
B. exhaust mode,
C. gas Land use models,
D. described percolator is purged with the exhaust of the percolator run with offset time from another,
E. percolator described in air purge is used,
F. described percolator is opened,
Wherein in exhaust mode, described water decomposition gas is extracted out from described percolator as exhaust, wherein in gas Land use models, water decomposition gas to be extracted out and for energy recovery from described percolator, and wherein in steps d. and the water decomposition gas that during middle purging, described percolator inside exists is rich in CO by utilizing to send to from the percolator discharge operated under offset time
2water decomposition gas driven away and removed, be wherein saidly rich in CO
2water decomposition gas there is the CO of at least 50 volume %
2content, and the methane content being less than 2 volume %.
2. method according to claim 1, is characterized in that described exhaust mode continues until the methane concentration of the inner gas existed of percolator reaches the methane concentration of at least 2 volume % and/or until the pH value of described hydrolyzate reaches pH value >5.
3. method according to claim 2, is characterized in that described gas Land use models continues until the methane concentration of the inner gas existed of described percolator is lower than 1 volume %.
4., according to the method one of claim 2 to 3 Suo Shu, the percolator that described in it is characterized in that, at least two operate under offset time operates in the mode making at least one percolator and operate with exhaust mode.
5. method according to claim 4, it is characterized in that before purging percolator, close and operate under offset time and another percolator operated with exhaust mode relative to percolator to be purged, make to produce overvoltage in this percolator, and after reaching pressure threshold, subsequently described exhaust is transported in percolator to be purged from the percolator operated under offset time.
6. in two levels, obtain the system of biogas, it comprises at least two percolator (P
1, P
2), its each self-contained hydrolyzate delivery pipe (2) and a liquid inlet opening (1), wherein hydrolyzate delivery pipe (2) is connected through at least one hydrolyzate storage tank (S) with at least one methane reactor (M), and wherein at least one fermented liquid storage tank (G) connected by fermentation liquid draining pipe (18) of at least one methane reactor arranged downstream described, wherein hydrolyzate storage tank (S) and fermented liquid storage tank (G) and percolator (P
1, P
2) respective liquid opening for feed (1) connect, at least two percolator (P described in it is characterized in that
1, P
2) be designed to airtight and each at least one closable feed tube (3) self-contained and at least one closable gas discharge pipe (4), and each percolator (P
1, P
2) be connected with methane transducer, described methane transducer is for measuring corresponding percolator (P
1, P
2) in the methane content of gas that exists, and it is connected with pH sensor (14), and described pH sensor is for measuring corresponding percolator (P
1, P
2) in the pH value of liquid that exists, and wherein each percolator (P
1, P
2) feed tube (3) be designed such that to allow to be switched to air supply, from another percolator gas supply or close feed tube, wherein said at least two percolator (P
1, P
2) be connected to each other by their gas supply pipe (3), make, with offset time run duration, a percolator (P in comfortable exhaust mode in future to occur
1) be rich in CO
2water decomposition gas send into percolator (P to be purged
2) in, wherein run with offset time and refer at least two percolators loading solid biogenic material under different initial time, and experience their Matrix lysis, make at least one percolator be in exhaust mode, described in be rich in CO
2water decomposition gas there is the CO of at least 50 volume %
2content, and the methane content being less than 2 volume %.
7. system according to claim 6, is characterized in that each percolator (P
1, P
2) comprising closable gas discharge pipe (4), wherein said gas discharge pipe (4) is designed to allow to be switched to by gaseous emission to energy utility system or discharge the exhaust in air or close described gas discharge pipe.
8. the system according to claim 6 or 7, is characterized in that at each percolator (P
1, P
2) place's layout pressure transmitter (17), it is for measuring percolator (P
1, P
2) inner pressure.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE102010028707.5A DE102010028707B4 (en) | 2010-05-06 | 2010-05-06 | Process and plant for gas-tight process control of percolators in a bi-or multi-stage biogas process |
| DE102010028707.5 | 2010-05-06 | ||
| PCT/EP2011/057282 WO2011138426A1 (en) | 2010-05-06 | 2011-05-06 | Method and system for the gas tight process control of percolators in a biogas method having two or more stages |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102959072A CN102959072A (en) | 2013-03-06 |
| CN102959072B true CN102959072B (en) | 2015-02-18 |
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| CN201180022822.4A Active CN102959072B (en) | 2010-05-06 | 2011-05-06 | Method and system for the gas tight process control of percolators in biogas method having two or more stages |
Country Status (7)
| Country | Link |
|---|---|
| US (1) | US8969032B2 (en) |
| EP (1) | EP2566946B1 (en) |
| CN (1) | CN102959072B (en) |
| CA (1) | CA2771678C (en) |
| DE (1) | DE102010028707B4 (en) |
| PL (1) | PL2566946T3 (en) |
| WO (1) | WO2011138426A1 (en) |
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| DE102011015415B4 (en) * | 2011-03-29 | 2018-11-15 | Karlsruher Institut für Technologie | Pressure methanization of biomass |
| DE102012212505A1 (en) * | 2012-07-17 | 2014-01-23 | Bekon Energy Technologies Gmbh & Co. Kg | Method for operating a biogas plant and a biogas plant operated in this way |
| DE102012108893A1 (en) * | 2012-09-20 | 2014-03-20 | Renergon International AG | Operating biogas plant, comprises fermenting stackable biomass, connecting digester gas space of the solid fermenter with gas line for discharging biogas, and performing inertization of fermenter gas space or gas line |
| DE102012222589A1 (en) | 2012-12-07 | 2014-06-12 | Planungsbüro Rossow Gesellschaft für erneuerbare Energien mbH | SUBSTRATE CIRCUIT FOR BIOGAS PLANTS IN A CONNECTION AND COMBI HYDROLYSIS CONTAINER |
| DE102013106953A1 (en) * | 2013-07-02 | 2015-01-08 | Peter Lutz | Biogas production from biomass |
| DE102013107754A1 (en) * | 2013-07-19 | 2015-01-22 | Peter Lutz | Biogas plant and procedures for its operation |
| DE102014011479A1 (en) | 2014-07-31 | 2016-02-04 | Christoph Bürger | New process for the fermentation of biogenic energy sources |
| DE102016003146A1 (en) * | 2016-03-15 | 2017-09-21 | Pöttinger Entsorgungstechnik GmbH & Co. KG | Process and apparatus for the production of biogas |
| CN109679829A (en) * | 2019-03-05 | 2019-04-26 | 山东鲁花生物科技有限公司 | A kind of seeding tank connection structure and its application method preventing miscellaneous bacteria cross contamination |
| DE102020204475A1 (en) * | 2020-04-07 | 2021-10-07 | Deere & Company | Method and arrangement for the production of silage |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101538176A (en) * | 2008-03-20 | 2009-09-23 | 贝肯能量科技两合公司 | Combined installation used for producing biogas and compost and switching method of fermenter thereof |
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| NL8303129A (en) * | 1983-09-09 | 1985-04-01 | Gist Brocades Nv | METHOD AND APPARATUS FOR ANAEROOB FERMENTATION OF SOLID WASTES IN TWO PHASES. |
| US5269634A (en) * | 1992-08-31 | 1993-12-14 | University Of Florida | Apparatus and method for sequential batch anaerobic composting of high-solids organic feedstocks |
| DE20104047U1 (en) | 2000-07-14 | 2001-10-25 | Bekon Energy Technologies Gmbh | Bioreactor for the methanation of biomass and a biogas plant for generating thermal, electrical or mechanical energy from biomass with such a bioreactor |
| FI116521B (en) * | 2002-05-21 | 2005-12-15 | Preseco Oy | Procedure for processing organic material |
| KR20060036603A (en) * | 2004-10-26 | 2006-05-02 | 서용석 | Polymeric composite separation membrane |
| DE102004053615B3 (en) | 2004-11-03 | 2006-05-18 | Brandenburgische Technische Universität Cottbus | Degradation of biogenic material |
| DE102006009165A1 (en) * | 2005-02-24 | 2007-01-11 | Christian Widmer | Waste material e.g. residual waste treatment method, involves converting and washing organic constituents in waste materials without aeration in reactor, and removed solid from organic |
| DE112006001877A5 (en) | 2005-07-26 | 2008-04-30 | GICON-Großmann Ingenieur Consult GmbH | Process and plant for the multistage hydrolysis of solid biogenic raw materials |
| US7556737B2 (en) * | 2005-12-16 | 2009-07-07 | The Regents Of The University Of California | Anaerobic phased solids digester for biogas production from organic solid wastes |
| DE102008007423B4 (en) * | 2008-02-01 | 2014-03-27 | Schmack Biogas Gmbh | Process for the production of biogas and biogas plant for carrying out the process |
| DE102008046879A1 (en) * | 2008-09-11 | 2010-03-25 | Schmack Biogas Ag | Process for biogas upgrading and biogas plant |
-
2010
- 2010-05-06 DE DE102010028707.5A patent/DE102010028707B4/en not_active Expired - Fee Related
-
2011
- 2011-05-06 US US13/696,169 patent/US8969032B2/en active Active
- 2011-05-06 CA CA2771678A patent/CA2771678C/en active Active
- 2011-05-06 WO PCT/EP2011/057282 patent/WO2011138426A1/en active Application Filing
- 2011-05-06 PL PL11719230T patent/PL2566946T3/en unknown
- 2011-05-06 CN CN201180022822.4A patent/CN102959072B/en active Active
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| CN101538176A (en) * | 2008-03-20 | 2009-09-23 | 贝肯能量科技两合公司 | Combined installation used for producing biogas and compost and switching method of fermenter thereof |
Also Published As
| Publication number | Publication date |
|---|---|
| US20130078700A1 (en) | 2013-03-28 |
| WO2011138426A1 (en) | 2011-11-10 |
| EP2566946A1 (en) | 2013-03-13 |
| US8969032B2 (en) | 2015-03-03 |
| CA2771678C (en) | 2016-08-23 |
| EP2566946B1 (en) | 2014-04-09 |
| CA2771678A1 (en) | 2011-11-10 |
| CN102959072A (en) | 2013-03-06 |
| DE102010028707A1 (en) | 2011-11-10 |
| PL2566946T3 (en) | 2014-09-30 |
| DE102010028707B4 (en) | 2014-12-18 |
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